EP0368835A1 - Procédé pour la production de la fonte liquide et installation pour la mise en oeuvre de ce procédé - Google Patents

Procédé pour la production de la fonte liquide et installation pour la mise en oeuvre de ce procédé Download PDF

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Publication number
EP0368835A1
EP0368835A1 EP89890270A EP89890270A EP0368835A1 EP 0368835 A1 EP0368835 A1 EP 0368835A1 EP 89890270 A EP89890270 A EP 89890270A EP 89890270 A EP89890270 A EP 89890270A EP 0368835 A1 EP0368835 A1 EP 0368835A1
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EP
European Patent Office
Prior art keywords
reduced
reducing gas
reduction
fraction
ore
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP89890270A
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German (de)
English (en)
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EP0368835B1 (fr
Inventor
Werner Dipl.-Ing. Dr. Kepplinger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Primetals Technologies Austria GmbH
Deutsche Voest Alpine Industrieanlagenbau GmbH
Original Assignee
Voest Alpine Industrienlagenbau GmbH
Deutsche Voest Alpine Industrieanlagenbau GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Voest Alpine Industrienlagenbau GmbH, Deutsche Voest Alpine Industrieanlagenbau GmbH filed Critical Voest Alpine Industrienlagenbau GmbH
Publication of EP0368835A1 publication Critical patent/EP0368835A1/fr
Application granted granted Critical
Publication of EP0368835B1 publication Critical patent/EP0368835B1/fr
Anticipated expiration legal-status Critical
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B11/00—Making pig-iron other than in blast furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
    • C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
    • C21B13/002—Reduction of iron ores by passing through a heated column of carbon
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

  • the invention relates to a process for the production of molten pig iron by melting reduction of iron ores of different grain sizes, which contain a fraction A with grain sizes corresponding to diameters of less than 0.2 mm, the ore being pre-reduced with reducing gas, the pre-reduced material being completely reduced and in a smelting gasifier is melted into molten pig iron, and a plant for carrying out the process.
  • Fine ores with a particle diameter of less than 0.5 mm can be reduced in a circulating fluidized bed, e.g. is described in DE-A - 25 21 038.
  • all of these processes are not suitable for processing iron ores with a wide grain band, as are e.g. Fine ores in unscreened form, or fine ores that have been screened from an ore coarse fraction.
  • Such ores cannot be processed on an industrial scale into pig iron without prior preparation in the cooking oven or by other smelting reduction processes. This applies in particular to fine ores that contain dust, whereby ore particles are understood that have a diameter of less than 0.2 mm (fraction A).
  • Such ores must be pre-ground before being smelted and agglomerated to a uniform grain size.
  • a method and a plant for the smelting reduction of fine ore is known from DE-C - 35 35 572, according to which the ore after passing through two not described in detail Pre-reduction units are fed to the melter at the level of the oxygen injection level.
  • this system is not suitable for processing fine ores which have a wide grain size range, since at least the dust-like ore fractions are entrained by the counter-flowing reducing gas and discharged again during charging into the first pre-reduction unit. A return of this share is not provided for in DE-C - 35 35 572.
  • the aim of the present invention is to eliminate these disadvantages in the processing of iron ores of different grain sizes, in particular with a dust content (fraction A), and to provide a method and a plant with which ores of a broad grain size spectrum can be obtained without pre-grinding and agglomeration melted into molten pig iron in a melter gasifier using the smelting reduction process can be.
  • the final reduction of fraction A advantageously takes place in a reduction cyclone into which the reducing gas loaded with the pre-reduced fraction A is passed. Due to the small diameter of the ore particles of fraction A, the short period of time which is usually required for separating a solid in a cyclone is sufficient for the finished reduction.
  • the remaining fraction B is likewise pre-reduced to a certain degree from the reducing gas during the separation of fraction A, the degree of pre-reduction being naturally smaller the larger the ore particles are.
  • Pre-reduced ore particles with a diameter of less than 2 mm can be easily reduced by passing them under reduced pressure through a fluidized bed through which reducing gas flows and then reducing them. After this treatment, ore particles of this size have practically the same high degree of metallization as fraction A after separation in the reduction cyclone, because they are in contact with the reducing gas comparatively longer in the fluidized bed.
  • the fluidized bed enables a faster and therefore more efficient reduction.
  • the two reduced fractions A and B are expediently melted into molten pig iron in a melter gasifier by feeding it to the melter gasifier in the region of the oxygen injection plane or above this plane in the region of the coke bed. Due to the high degree of metallization of the reduced fractions A and B, the melter gasifier requires less heat to produce the liquid pig iron.
  • fraction B contains grain sizes corresponding to a maximum diameter of 5 mm
  • this fraction is also advantageously passed through a fluidized bed through which reducing gas flows, after which fraction B1, which has grain sizes corresponding to a diameter of less than 2 mm, is separated and fraction B2, which Has grain sizes corresponding to diameters of at least 2 mm, additionally passed under the influence of gravity through a fixed bed through which reducing gas flows and is further reduced in the process.
  • fraction B additionally contains grain sizes corresponding to a diameter of up to 20 mm, preferably up to 10 mm
  • the proportion B2 which in this case has particles with a diameter of 2 mm to 20 mm, preferably 2 mm to 10 mm , expediently introduced into the settling zone of the melter gasifier, which is located above its fluidized bed.
  • a system for carrying out the method according to the invention consists of the combination of a meltdown gasifier with a reduction cyclone, the reduction cyclone on the discharge side being connected to the lower part of the meltdown gasifier via a transport device for reduced iron ore and a reduction gas line leading from the settling space of the meltdown gasifier to the reduction cyclone.
  • Such a system is particularly suitable for the cost-effective processing of dust ores or fine ores with grain sizes corresponding to a diameter of up to 0.5 mm.
  • the plant according to the invention is further distinguished by its compactness.
  • a preferred embodiment of the plant according to the invention is characterized in that a reduction reactor is interposed in the reducing gas line between the melting gasifier and the reducing cyclone, which has a fluidized bed formed by the reducing gas and optionally also a fixed bed and is connected to the melting gasifier on the discharge side via at least one transport device for reduced iron ore.
  • a reduction reactor is interposed in the reducing gas line between the melting gasifier and the reducing cyclone, which has a fluidized bed formed by the reducing gas and optionally also a fixed bed and is connected to the melting gasifier on the discharge side via at least one transport device for reduced iron ore.
  • FIGS. 1 to 4 each schematically showing particular embodiments of the system according to the invention.
  • Fig. 1 is a melter gasifier, which in the embodiment shown has a lower section 1 ', has a central section 1 ⁇ and an expanded upper section 1 ′′′.
  • the lower section 1 ' is intended for receiving the molten bath.
  • In the middle section 1 ⁇ open nozzles 2 (burner) with a feed line 3 for oxygen.
  • a feed line 4 for carbon-containing material and a line 5 for reduced ore also open in the immediate area of the nozzle level.
  • This line 5 can alternatively also open above the nozzle level in the area of the upper coke bed II into the melter gasifier 1, as in FIG Line 5 'is indicated by dashed lines.
  • the melter gasifier 1 has charging devices 6 for lumpy coal with grain sizes corresponding to a diameter of up to 40 mm, 7 for ore and 8 for additives. Furthermore, a reducing gas line 9 is provided in the upper section 1 für for the discharge of reducing gas formed in the melter gasifier.
  • the fixed beds (fixed bed zones) designated I and II are formed from coarser coke particles.
  • the melt pool that accumulates underneath consists of the molten metal 10 and slag 11, a tap being provided for each of the two components.
  • the fixed bed I has no gas supply, so it is not gas.
  • the fixed bed II is formed, in which the coke particles are flowed through by the oxygen-containing gas flowing out of the feed line 3 with the formation of carbon monoxide.
  • a fluidized bed III is formed above the fixed bed II and is kept in motion by the reducing gas generated in the fixed bed II. Small coal or coke particles remain in the fluid bed zone III. Larger coal or coke particles for which the empty pipe speed of the gas flow is below the loosening point for a corresponding particle bed, are only slowed down, fall through the fluidized bed III and settle to form the fixed bed II or the fixed bed I.
  • the calming zone IV is located above the fluidized bed III. the iron ore is being charged.
  • a reduction cyclone 12 with a reduction cyclone is referred to, in which the reducing gas line 9 and a charging device 13 for additives open.
  • a discharge device 14 for reduced dust ore 14 ' is provided, which is applied to the line 5.
  • Suspended, reduced dust ore is removed from the top part of the reduction cyclone through the top gas line 15, cooled in the cooler 16, compressed in the cooling gas blower 17 and either via the return line 18 into the reduction gas line 9 for cooling the gas dust ore suspension from the melter gasifier 1 , or fed via line 19 by means of injector 20 into line 5.
  • the branch line 15 'top gas of the system can also be removed and fed to other uses.
  • the embodiment of the plant according to the invention shown in FIG. 1 is suitable for processing fine iron ores with a grain size corresponding to a maximum diameter of 0.5 mm, but especially for dust ores, the ore particles having a diameter of less than 0.2 mm (fraction A) .
  • Such ore is charged into the calming zone (IV) of the melter gasifier 1, which has a temperature of about 1000 ° C. in the upper part of the calming zone (IV), where it is pre-reduced by the counter-flowing reducing gas which is formed in the lower part of the melter gasifier becomes.
  • the pre-reduced fraction A is almost completely entrained by the reducing gas and introduced into the reducing cyclone 12 through the reducing gas line 9, the gas dust ore suspension being cooled to a temperature of about 800 ° C. at this point in time.
  • fraction A is reduced with reducing gas and separated from the reducing gas by the cyclone effect.
  • the reduced fraction A is applied via the discharge device 14 of the line 5 and blown with top gas directly into the melting zone of the melter gasifier, etc. either in the area of the oxygen injection level or above, in the area of the coke bed II.
  • the fine ore fraction remaining in the calming zone IV of the melter gasifier 1 with a particle diameter of at least 0.2 mm (and maximum 0.5 mm) is also pre-reduced in the calming zone, but cannot be discharged by the reducing gas stream and passes through the fluidized bed III as a result of gravity into the fixed bed II or I is reduced and melted.
  • Ore fractions with a particle diameter of more than 0.5 mm cannot be processed with the system shown in FIG. 1, since they can no longer be satisfactorily reduced in the melter gasifier.
  • FIG. 2 The processing of such an ore allows the embodiment of the plant according to the invention shown in FIG. 2. It differs from the variant according to FIG. 1 mainly in that a reduction reactor 21 is interposed in the reduction gas line 9 between the melter gasifier 1 and the reduction cyclone 12, the charging devices 13 'for additives and 7' for contains the ore and has a discharge device 22 for reduced ore.
  • a reduction reactor 21 is interposed in the reduction gas line 9 between the melter gasifier 1 and the reduction cyclone 12, the charging devices 13 'for additives and 7' for contains the ore and has a discharge device 22 for reduced ore.
  • a fluid bed V of ore with reducing gas from the melter gasifier 1 is maintained, which is blown into the nozzle plane 23, which are fed by the reducing gas line 9.
  • the calming zone VI is located above the fluidized bed V.
  • a line 24 for completely reduced fine ore connects to the discharge device 22 and opens into the line 5.
  • the embodiment of the plant according to the invention shown in FIG. 2 is particularly suitable for processing fine ores which have ore particles with a diameter of up to 1 mm.
  • This ore is charged by means of the charging device 7 'in the calming zone VI of the reduction reactor 21 and partially pre-reduced by the counter-flowing reducing gas which is generated in the melter gasifier 1 and is blown through the reducing gas line 9 into the lower part of the reduction reactor 21 and thereby maintains the fluidized bed V.
  • the reducing gas is passed through the further reducing gas line 9, which leads away from the upper part of the reducing reactor 21, into the reducing cyclone, thereby entraining the pre-reduced fraction A.
  • This is finished reduced in the reduction cyclone 12 and, as described with reference to FIG. 1, fed to the melter gasifier 1.
  • the reduction reactor 21 is advantageously conical at least in the lower part, as a result of which the reducing gas has different flow velocities when it is passed through, which supports the separation of the two ore fractions.
  • the larger diameter of the particles of fraction B they have about the same high degree of metallization after discharge from the reduction reactor as the fraction A reduced in the reduction cyclone 12, because the larger particles in the fluidized bed have been in contact with the reducing gas for a sufficiently long time.
  • the fraction B which in the present case has ore particles with a diameter of 0.2 mm to 5 mm, passes through the fluidized bed V, the ore particles with a diameter of less than 2 mm substantially reduced and therefore by means of the discharge device 25 ' lower part of the fluidized bed V removed, acted on via line 25 of line 5 and together with the reduced fraction A - as described above - can be fed to the melter 1.
  • the pre-reduced ore fraction remaining in the fluidized bed V passes by gravity to the fixed bed VII and further through it, the ore being further reduced. Finally, it is acted upon by means of the discharge device 22 'of the line 24' and with top gas which is taken from the line 19 ', via the injector 20' the melter gasifier 1 into the boundary region between the fluidized bed III and the upper fixed bed II (reduction zone of the melter gasifier) blown in and reduced or melted pig iron.
  • the reactor 21 shown in Fig. 3 is not only conical in the lower part, there are also two injection planes 23 and 23 'for the reducing gas, via which the strength of the gas supply and thus the different rates of rise and fall of the grain fractions are controlled can. It has been shown that for an optimal separation effect, the boundary between ore fixed bed VII and ore fluidized bed V in conical area, leveling between the two injection levels 23 and 23 '.
  • the fluidization, fractionation and reduction of the small ore particles is primarily achieved, while the reducing gas supplied via the lower level 23 'primarily reduces the coarse fraction of the ore.
  • a cyclone 27 is provided in the variant of the plant according to the invention shown in FIG. 4 for the separation of possibly entrained coal dust, which acts on the discharge device 28 of the line 29 and by means of cooling gas the melter gasifier 1 in its upper one Area of the fluid bed III or in its calming zone IV is blown.
  • the injection nozzles 30 also have a supply 31 for oxygen.
  • the cooling gas is reducing gas freed from coal dust from the melter gasifier 1, which is removed from the reducing gas line 9, cooled in the cooler 32, fed to the cooling gas blower 34 via the cooling gas line 33, compressed and finally discharged to the line 29.
  • the cooling gas can also be returned to the line 35 Reduction gas line 9 are fed back.
  • nitrogen can also be used for blowing in the coal dust, which nitrogen can be supplied to the line 29 at any point.
  • the reducing gas After the reducing gas has passed the cooler 32, it can also be fed to the top gas line 37 via the line 36.
  • the operation of the variant of the plant according to the invention shown in FIG. 4 corresponds to that described in FIG. 3: the ore is charged into the reduction reactor 21, fraction A is discharged with reducing gas, completely reduced in the reduction cyclone 12 and fed to the melter gasifier as described above, the fully reduced fractions can be blown with top gas, nitrogen or another inert gas.
  • the ore remaining in the settling zone of the reduction reactor 21 reaches the ore fluidized bed V under the action of gravity, in which those ore particles which have a diameter of less than 2 mm are practically completely reduced and discharged from the fluidized bed V.
  • the remaining ore passes through the ore fixed bed VII, which in the embodiment shown in FIG.
  • the empty pipe speeds in the melter gasifier 1 and in the reduction reactor 21 were between 0.3 and 0.5 m / s, whereas the empty pipe speed between the two nozzle levels of the reduction reactor 21 was 1.5 to 3 m / s.
  • the pig iron obtained had the following constituents: C. 4% Si 0.6% phosphorus 0.01% manganese 0.1% sulfur 0.04%
EP89890270A 1988-10-25 1989-10-16 Procédé pour la production de la fonte liquide et installation pour la mise en oeuvre de ce procédé Expired - Lifetime EP0368835B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT2642/88 1988-10-25
AT0264288A AT390622B (de) 1988-10-25 1988-10-25 Verfahren und anlage zur herstellung von fluessigem roheisen

Publications (2)

Publication Number Publication Date
EP0368835A1 true EP0368835A1 (fr) 1990-05-16
EP0368835B1 EP0368835B1 (fr) 1994-03-09

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EP89890270A Expired - Lifetime EP0368835B1 (fr) 1988-10-25 1989-10-16 Procédé pour la production de la fonte liquide et installation pour la mise en oeuvre de ce procédé

Country Status (16)

Country Link
US (1) US4978387A (fr)
EP (1) EP0368835B1 (fr)
JP (1) JP2955306B2 (fr)
KR (1) KR0129765B1 (fr)
CN (1) CN1022048C (fr)
AT (1) AT390622B (fr)
AU (1) AU626325B2 (fr)
BR (1) BR8905412A (fr)
CA (1) CA1338125C (fr)
CZ (1) CZ279991B6 (fr)
DD (1) DD297844A5 (fr)
DE (2) DE3932182C2 (fr)
RU (1) RU1813099C (fr)
SK (1) SK278799B6 (fr)
UA (1) UA15505A (fr)
ZA (1) ZA897703B (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
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EP0576414A1 (fr) * 1992-05-21 1993-12-29 Voest-Alpine Industrieanlagenbau Gmbh Procédé pour la production de la fonte liquide ou des ébauches en acier ainsi que dispositif pour la mise en oeuvre de ce procédé
EP0594557A1 (fr) * 1992-10-22 1994-04-27 VOEST-ALPINE Industrieanlagenbau GmbH Procédé pour produire de la fonte brute liquide ou des produits d'acier préaffinés liquides
EP0864658A1 (fr) * 1997-03-13 1998-09-16 The Boc Group, Inc. Reduction de minerai de fer
WO1999032667A1 (fr) * 1997-12-22 1999-07-01 Pohang Iron & Steel Co., Ltd. Dispositif destine a charger directement du minerai de fer fin reduit dans un four de fusion-gaseificateur
WO2010069711A1 (fr) * 2008-12-19 2010-06-24 Siemens Vai Metals Technologies Gmbh & Co Procédé de fabrication de métaux liquides
EP2631305A1 (fr) * 2012-07-09 2013-08-28 Siemens VAI Metals Technologies GmbH Composition de procédé de réduction d'une couche à turbulences et procédé de réduction directe

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DE3723137C1 (de) * 1987-07-13 1989-03-16 Voest Alpine Ind Anlagen Vorrichtung zur Beschickung eines Einschmelzvergasers mit Vergasungsmitteln und Eisenschwamm
DE4041936C1 (fr) * 1990-12-27 1992-09-24 Deutsche Voest-Alpine Industrieanlagenbau Gmbh, 4000 Duesseldorf, De
BE1006828A3 (fr) * 1991-07-12 1995-01-03 Elsen Tooling Ireland Ltd Procede en vue de la preparation de metaux, et en particulier de fer, a partir de minerais oxydes, a une temperature de reduction quelconque, dans un four de reduction a gouttes.
US5320676A (en) * 1992-10-06 1994-06-14 Bechtel Group, Inc. Low slag iron making process with injecting coolant
US6197088B1 (en) 1992-10-06 2001-03-06 Bechtel Group, Inc. Producing liquid iron having a low sulfur content
US5397376A (en) * 1992-10-06 1995-03-14 Bechtel Group, Inc. Method of providing fuel for an iron making process
US5354356A (en) * 1992-10-06 1994-10-11 Bechtel Group Inc. Method of providing fuel for an iron making process
DE4240194C1 (de) * 1992-11-30 1994-06-01 Bogdan Dipl Ing Vuletic Verfahren zur Herstellung von Roheisen aus Feinerz und Vorrichtung zu seiner Durchführung
DE4326562C2 (de) * 1993-08-07 1995-06-22 Gutehoffnungshuette Man Verfahren und Vorrichtung zur Direktreduktion von Feinerzen bzw. Feinerzkonzentraten
US5958107A (en) * 1993-12-15 1999-09-28 Bechtel Croup, Inc. Shift conversion for the preparation of reducing gas
KR100226897B1 (ko) * 1994-12-26 1999-10-15 이구택 용철제조용 고온 예비환원 분철광석의 괴성화방법
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AT403381B (de) 1996-06-10 1998-01-26 Voest Alpine Ind Anlagen Verfahren und anlage zum chargieren von metallträgern in eine einschmelzvergasungszone
KR100276324B1 (ko) * 1996-12-20 2000-12-15 이구택 용융환원 장치 및 이를 이용한 용융선철 제조방법
KR100264993B1 (ko) 1996-12-23 2000-09-01 이구택 산소풍구전단에 형성되는 침투길이의 최적유지 장치 및 방법
DE19706348C1 (de) * 1997-02-07 1998-09-03 Ferrostaal Ag Vorrichtung zur Direktreduktion von Feinerzen
BR9710465A (pt) 1997-05-02 1999-08-17 Po Hang Iron & Steel Aparelho e m-todo para fabricar ferro fundido usando forno de calcina-Æo
JP2000510537A (ja) 1997-12-20 2000-08-15 ポーハング アイアン アンド スティール シーオー．，エルティディ． 流動床を使用することにより溶融銑鉄及び還元鉄を製造するための装置、並びにそのための方法
US6224649B1 (en) 1998-07-06 2001-05-01 Hylsa, S.A. De C.V. Method and apparatus for reducing iron-oxides-particles having a broad range of sizes
US6132489A (en) * 1998-07-06 2000-10-17 Hylsa, S.A. De C.V. Method and apparatus for reducing iron-oxides-particles having a broad range of sizes
AT407052B (de) * 1998-08-13 2000-12-27 Voest Alpine Ind Anlagen Verfahren zur herstellung von flüssigem roheisen
UA70348C2 (uk) 1999-11-04 2004-10-15 Пхохан Айрон Енд Стіл Ко., Лтд. Відновний реактор з псевдозрідженим шаром і спосіб стабілізації псевдозрідженого шару у такому реакторі
KR100368287B1 (ko) * 2000-08-23 2003-01-24 주식회사 포스코 일반탄 및 분철광석을 이용한 용철제조설비에서 미분광석추가장입장치
KR100584732B1 (ko) * 2001-04-27 2006-05-30 주식회사 포스코 일반탄을 이용하는 용철제조공정에서의 폐기물 재활용방법
AT411265B (de) * 2002-02-14 2003-11-25 Voest Alpine Ind Anlagen Verfahren und vorrichtung zur erzeugung von metallen und/oder metallvorprodukten
US20050151307A1 (en) * 2003-09-30 2005-07-14 Ricardo Viramontes-Brown Method and apparatus for producing molten iron
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AT413821B (de) * 2004-12-23 2006-06-15 Voest Alpine Ind Anlagen Verfahren und vorrichtung zur erzeugung von metallen und/oder metallvorprodukten
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EP0576414A1 (fr) * 1992-05-21 1993-12-29 Voest-Alpine Industrieanlagenbau Gmbh Procédé pour la production de la fonte liquide ou des ébauches en acier ainsi que dispositif pour la mise en oeuvre de ce procédé
US5445668A (en) * 1992-05-21 1995-08-29 Voest-Alpine Industrieanlagenbau G.M.H Method of producing molten pig iron or molten steel pre-products
EP0594557A1 (fr) * 1992-10-22 1994-04-27 VOEST-ALPINE Industrieanlagenbau GmbH Procédé pour produire de la fonte brute liquide ou des produits d'acier préaffinés liquides
US5584910A (en) * 1992-10-22 1996-12-17 Pohang Iron & Steel Co., Ltd. Process for producing molten pig iron or molten steel pre-products
EP0864658A1 (fr) * 1997-03-13 1998-09-16 The Boc Group, Inc. Reduction de minerai de fer
WO1999032667A1 (fr) * 1997-12-22 1999-07-01 Pohang Iron & Steel Co., Ltd. Dispositif destine a charger directement du minerai de fer fin reduit dans un four de fusion-gaseificateur
US6235080B1 (en) 1997-12-22 2001-05-22 Pohang Iron & Steel Co. Ltd. Charging device for directly charging reduced fine iron ore into melter-gasifier
WO2010069711A1 (fr) * 2008-12-19 2010-06-24 Siemens Vai Metals Technologies Gmbh & Co Procédé de fabrication de métaux liquides
EP2631305A1 (fr) * 2012-07-09 2013-08-28 Siemens VAI Metals Technologies GmbH Composition de procédé de réduction d'une couche à turbulences et procédé de réduction directe

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DE3932182C2 (de) 1995-03-16
RU1813099C (ru) 1993-04-30
JPH02156010A (ja) 1990-06-15
KR0129765B1 (ko) 1998-04-17
JP2955306B2 (ja) 1999-10-04
CN1042185A (zh) 1990-05-16
CN1022048C (zh) 1993-09-08
SK590989A3 (en) 1998-03-04
BR8905412A (pt) 1990-05-22
SK278799B6 (sk) 1998-03-04
CA1338125C (fr) 1996-03-12
AU626325B2 (en) 1992-07-30
DD297844A5 (de) 1992-01-23
AU4248289A (en) 1990-05-03
KR900006525A (ko) 1990-05-08
DE3932182A1 (de) 1990-04-26
DE58907174D1 (de) 1994-04-14
AT390622B (de) 1990-06-11
US4978387A (en) 1990-12-18
ATA264288A (de) 1989-11-15
UA15505A (uk) 1997-06-30
CZ279991B6 (cs) 1995-09-13
ZA897703B (en) 1990-07-25
EP0368835B1 (fr) 1994-03-09
CZ590989A3 (en) 1995-04-12

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